CN1556174A - Production method of biodiesel oil using high acid ralue animal and vegetable grease - Google Patents
Production method of biodiesel oil using high acid ralue animal and vegetable grease Download PDFInfo
- Publication number
- CN1556174A CN1556174A CNA2003101116967A CN200310111696A CN1556174A CN 1556174 A CN1556174 A CN 1556174A CN A2003101116967 A CNA2003101116967 A CN A2003101116967A CN 200310111696 A CN200310111696 A CN 200310111696A CN 1556174 A CN1556174 A CN 1556174A
- Authority
- CN
- China
- Prior art keywords
- acid value
- glycerine
- high acid
- oil
- plant oil
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Liquid Carbonaceous Fuels (AREA)
- Fats And Perfumes (AREA)
Abstract
A process for preparing the biological diesel oil from the animal fat or vegetative oil with high acid number includes esterifying by glycerine under existance of strong acid catalyst, distilling in azeotropic solvent for removing water, mixing with methanol, transesterifying reacting to remove glycerine, water washing, and low-temp treating for removing high-smelting-point substances to obtain methyl ester of fatty acid, which is just the biological diesel oil.
Description
Technical field
The present invention relates to a kind of with high acid value animal-plant oil production fatty acid methyl ester---method of bio-diesel oil, genus field of grease chemical technology.
Background technology
Acid number is one of important indicator of reflection animal-plant oil quality, and acid number surpasses certain limit indication grease and is not suitable for eating, and is called high-acid value grease, and (mainly contain: the waste grease behind the fried food often claims old oil as discarded food oils; The grease that the food and drink water drain reclaims, i.e. sewer oil or the swill oil of often saying), the long-term deposit of grease surpasses rotten grease of quality guaranteed period acidifying and recovery obtains from the various oil foots of edible oil factory grease etc. and all possesses this feature.The technology of utilizing about the high acid value animal-plant oil has more report.
In disclosed technology, as described in CN1382762A, it is under an acidic catalyst existence condition, the aste vegetable oil and animal fat of various different acid numbers is carried out alcoholysis and esterification, after passing through a series of processing then, employing adds soda ash distillatory method and produces fatty acid methyl ester---method of bio-diesel oil, and distillation temperature is up to 320 ℃, and this Technology Energy consumption is the emphasis that needs consideration.CN1370140A is described, it is a kind of single-phase process for preparing fatty acid methyl ester by tri-glyceride and lipid acid, adopt cosolvent that esterification is carried out under single-phase condition, wherein alcohol is 15: 1 to 35: 1 with the molar ratio range of tri-glyceride and lipid acid, the yield of its unreacting alcohol is very big, industrial significance is little, and glycerine is not considered to reclaim yet.CN1031070C is described, is the technology of raw material production fatty acid alkyl ester with the natural fats and oils that contains free fatty acids, and in the presence of acid catalyst, natural fats and oils is being higher than under the alkanol boiling temperature and continuous C by reactor
1-C
4Reaction of alkanol, until the acid value of reaction mixture less than 1, then and C
1～4Monohydroxy-alcohol carries out back flow reaction in the presence of alkaline catalysts, obtain fatty acid alkyl ester, and this method will have a large amount of moisture C
1-C
4Alkanol produces, thereby needs extra energy to carry out C
1-C
4Alkanol reclaims.
Produce fatty acid methyl ester---biofuel for the high acid value animal-plant oil, all there is different defectives in prior art, in addition as being used for the derv fuel oil raw material, prior art is not all considered the cold filter clogging temperature of biofuel, cold filter clogging temperature is meant that vehicle fuel is cooled to the top temperature that begins to stop up the engine filter screen under prescribed condition, fatty acid methyl ester by existing technique known method production---biofuel is used at low temperatures and is had the settling generation, stop up the filter screen and the oil circuit of diesel motor, this is the common issue with during existing biofuel is used.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of high acid value animal-plant oil that can utilize economically to produce fatty acid methyl ester---method of bio-diesel oil, and this production method has transformation efficiency height, characteristic of low energy consumption.
The present invention for the technical scheme that problem adopted of the above-mentioned proposition of solution is:
(1) the high acid value animal-plant oil is mixed in having the conversion unit of condensation reflux unit with glycerine, the acid value of high acid value animal-plant oil is at 10～150mgKOH/g oil, according to the acid value difference, the add-on of glycerine and the mol ratio of the free fatty acids in the oil are 0.35～2.0, add strong acid simultaneously as catalyzer, add binary azeotropic solvent distillation or ternary azeotropic solvent distillation again, the add-on of azeotropic distillation solvent is 15～60% of high acid value animal-plant oil by weight
(2) stirring heating is carried out back flow reaction, the moisture that reaction generates is taken out of by azeotropic distillation solvent, and water separates automatically with solvent after the condensation, and azeotropic distillation solvent refluxes back in the conversion unit, water is then discharged, take reactor reaction out of until no moisture and finish, steam azeotropic distillation solvent, get esterification mixture, back flow reaction is carried out under normal pressure, the back flow reaction temperature depends on the azeotropic distillation solvent of employing between 60～120 ℃
(3) behind the esterification mixture and catalyst separating that process (2) is obtained, adopt discoloring agent then to esterification mixture decolouring processing,
(4) esterification mixture after the decolouring, (amount of corresponding esterification mixture) adds 15～30% methyl alcohol by weight, and 0.5～1.2% alkali catalyst is 60～80 ℃ in temperature and carries out transesterification,
(5) mixture that obtains of transesterification adopts centrifugation to go out raw glycerine, and raw glycerine is after acidifying separates, and the glycerine that part contains free fatty acids returns the esterification that esterifier is participated in process (1), and most of raw glycerine carries out glycerine and reclaims,
(6) fatty acid methyl ester after the separation of glycerin removes the free glycerol of trace with 30～45% hot wash, superfluous unreacted methanol is also dissolved in the water and is taken out of, centrifugation must be washed fatty acid methyl ester (thick ester), the water of separating distills out methyl alcohol and returns the methyl alcohol storage tank, and the hot wash temperature is controlled at 60～95 ℃.
Press such scheme, can carry out winterization in the winterization machine to the washing fatty acid methyl ester, the winterization temperature is-5～3 ℃, separates the high melting-point material after the winterization, obtains purified fatty acid methyl ester---the biofuel product.
In the such scheme, described high acid value animal-plant oil can be the grease of various recovery, the rotten grease of frying oil that reclaims as catering trade and sewer oil, long-term deposit, restored acid carburetion from the oil-fat plant oil foot.
Press such scheme, according to the acid value difference, the ratio that adds glycerine changes, and the mol ratio of free lipid acid is 0.8～1.3 in preferred glycerine add-on and the oil.
Press such scheme, described strong acid is the vitriol oil of concentration 98%, add-on is 0.8～1.2% of high acid value animal-plant oil by weight, perhaps is macroporous type polystyrene storng-acid cation exchange resin, and add-on is 5～10% of high acid value animal-plant oil by weight.
Press such scheme, described binary azeotropic solvent distillation is benzene,toluene,xylene, hexanaphthene, pentane or the ethyl acetate that forms binary azeotrope with water; Described ternary azeotropic solvent distillation is the ethanol and the hexanaphthene of the ethanol of the ternary azeotropic compositions that forms with water and benzene or the ternary azeotropic compositions that forms with water, azeotropic distillation solvent adds the moisture that is beneficial to the reaction generation to be taken out of from reactive system, and the moisture of taking out of from reactive system separates with azeotropic distillation solvent easily.The azeotropic distillation solvent add-on is too little, is unfavorable for circulation, and too high then later stage power consumption is bigger, and more excellent scope is 25～40%.
Press such scheme, described discoloring agent is atlapulgite or activated carbon.
Press such scheme, described alkali catalyst can be sodium methylate, NaOH or KOH, adopts NaOH, KOH to make alkali catalyst and should adopt its solid and dissolve in methyl alcohol in advance that to make alkali concn be 5～8% methanol solution.
The present invention at first mixes the high acid value animal-plant oil with glycerine, make catalytic esterification under the catalyzer condition adopting strong acid such as sulfuric acid or macroporous type polystyrene storng-acid cation exchange resin, add azeotropic distillation solvent during esterification and under reflux state, dewater, reduce free fatty acid content; In the presence of the highly basic transesterification catalyst, react the production fatty acid methyl ester with methyl alcohol then; Separate high melting-point material production method of bio-diesel oil by winterization at last.
Beneficial effect of the present invention is: first aspect is to adopt the free fatty acids that is difficult in evaporable alcohol as glycerol (glycerine) and the high-acid value grease than low-carbon alcohol such as methyl alcohol to carry out esterification, generate glycerin fatty acid ester, glycerin fatty acid ester regenerates glycerine behind transesterification, thereby realize the circulation and the recovery of glycerine, help the reduction of production cost; Second aspect is that the moisture that esterification generates adopts the organic solvent of insoluble entry to remove by component distillation, thereby guarantee high conversion rate of esterification, and energy efficient, because the moisture that esterification generates can be removed completely, guaranteed the high-level efficiency of esterification and transesterification; The 3rd aspect is to use winterization equipment, the high melting-point material in the fatty acid methyl ester removed, thereby make biofuel that good low temperature use properties be arranged.The inventive method is to seek a kind ofly can produce cold filter clogging temperature suitable fatty acids methyl esters---method of bio-diesel oil economically, can reclaim the glycerine that reaction generates simultaneously effectively.
The advantage of the technology of the present invention is significantly, and the evaporable alcohol (considering the recovery and the circulation preferably glycerine of glycerine) that is difficult to that can be less replaces a large amount of excessive low-carbon alcohol such as methyl alcohol, does not have the low-carbon alcohol processes such as aqueous methanol excessive in the esterification process that steam; And, improve the esterification transformation efficiency, thereby make the present technique economy better because the moisture that esterification generates is also constantly taken reactive system out of.
Embodiment
Embodiment 1
In the esterification device of taking back stream and water trap, 500 parts of the fast food frying oils that adding is reclaimed, its acid value is a 20mgKOH/g oil, add 14 parts of glycerine simultaneously, 150 parts of toluene, 5.20 parts in sulfuric acid, be heated to 92 ℃ and begin to reflux, observe the water trap phase interface, improve back flow reaction temperature to 115 ℃ gradually, do not go up to the water trap phase interface, esterification finishes, and in about 45 minutes of reaction times, emits the water in the water trap, closing volume steams toluene simultaneously.It is 1.68mgKOH/g oil that esterification mixture is surveyed acid value.Isolate strong acid then as catalyzer.
120 ℃ of decolourings 30 minutes, centrifugation filtered out atlapulgite to esterification mixture with 36 parts of atlapulgites.
With the esterification mixture transesterification device of packing into, under agitation and be heated to 65 ℃, in the transesterification device, add earlier 50 parts of methyl alcohol, add 70 parts of 7.2% NaOH methanol solutions again, continue to stir after 30 minutes, stop to stir, glycerine begins to separate out, and standing and reacting 2 hours is isolated lower floor's glycerine phase, ester separates in whizzer, and glycerine is further separated.
After the separation of glycerin, add 30% hot water buffered soln washing, tell hot water buffered soln and must wash thick ester; In the winterization machine, reduce the temperature to-4 ℃ then, take out centrifugation, get fatty acid methyl ester---436 parts of biofuel products.
Separate the glycerine obtain, add sulfuric acid acidation after, upper strata free fatty acids and glycerine tell that to give over to the esterification process circulation standby, are reclaimed after lower floor's glycerine separate solid particles.
Methyl alcohol, methyl alcohol reuse are reclaimed in the distillation of hot water buffered soln.
Embodiment 2
In taking back the stream and the esterification device of water trap, adding 500 parts of restored acid carburetion from vegetable seed source mill soap stock, its acid value is a 115mgKOH/g oil, add 73 parts of glycerine, 150 parts of toluene, 5.88 parts in sulfuric acid simultaneously, be heated to 92 ℃ and begin to reflux, observe the water trap phase interface, improve back flow reaction temperature to 115 ℃ gradually, do not go up to the water trap phase interface, esterification finishes, and in about 118 minutes of reaction times, emits the water in the water trap, closing volume steams toluene simultaneously.It is 1.82mgKOH/g oil that esterification mixture is surveyed acid value.Isolate strong acid then as catalyzer.
120 ℃ of decolourings 30 minutes, centrifugation filtered out atlapulgite to esterification mixture with the 40g atlapulgite.
With the esterification mixture transesterification device of packing into, under agitation and be heated to 65 ℃, in the transesterification device, add earlier 70 parts of methyl alcohol, add 72 parts of 7.2% NaOH methanol solutions again, continue to stir after 30 minutes, stop to stir, glycerine begins to separate out, and standing and reacting 2 hours is isolated lower floor's glycerine phase, ester separates in whizzer, and glycerine is further separated.
After the separation of glycerin, add 30% hot water buffered soln washing, tell hot water buffered soln and must wash thick ester; In the winterization machine, reduce the temperature to-4 ℃ then, take out centrifugation, get fatty acid methyl ester---437 parts of biofuel products.
Separate the glycerine obtain, add sulfuric acid acidation after, upper strata free fatty acids and glycerine tell that to give over to the esterification process circulation standby, are reclaimed after lower floor's glycerine separate solid particles.
Methyl alcohol, methyl alcohol reuse are reclaimed in the distillation of hot water buffered soln.
Embodiment 3
In the esterification device of taking back stream and water trap, adding 500 parts of restored acid carburetion from vegetable seed source mill soap stock, its acid value is a 115mgKOH/g oil, add 77 parts of glycerine simultaneously, 150 parts of 1: 4 ethanol benzene azeotropic solvent distillations, 20 parts of the macroporous type polystyrene storng-acid cation exchange resins of activated and methanol wash, being heated to 75 ℃ begins to reflux, observe the water trap phase interface, improve back flow reaction temperature to 100 ℃ gradually, do not go up to the water trap phase interface, esterification finishes, and in about 136 minutes of reaction times, emits the water in the water trap, closing volume steams solvent simultaneously.It is 1.97mgKOH/g oil that esterification mixture is surveyed acid value.Separating and filtering falls the resin as catalyzer then.
120 ℃ of decolourings 30 minutes, centrifugation filtered out activated carbon to esterification mixture with 40 parts of activated carbon.
With the esterification mixture transesterification device of packing into, under agitation be heated to 65 ℃, in the transesterification device, add earlier 73 parts of methyl alcohol, add 70 parts of 7.2% NaOH methanol solutions again, continue to stir after 30 minutes, stop to stir, glycerine begins to separate out, and standing and reacting 2 hours is isolated lower floor's glycerine phase, ester separates in whizzer, and glycerine is further separated.
After the separation of glycerin, add 30% hot water buffered soln washing, tell hot water buffered soln and must wash thick ester; In the winterization machine, reduce the temperature to-4 ℃ then, take out centrifugation, get fatty acid methyl ester---447 parts of biofuel products.
Separate the glycerine obtain, add sulfuric acid acidation after, upper strata free fatty acids and glycerine tell that to give over to the esterification process circulation standby, are reclaimed after lower floor's glycerine separate solid particles.
Methyl alcohol, methyl alcohol reuse are reclaimed in the distillation of hot water buffered soln.
Claims (9)
1, a kind of high acid value animal-plant oil production method of bio-diesel oil of utilizing is characterized in that:
(1) the high acid value animal-plant oil is mixed in having the conversion unit of condensation reflux unit with glycerine, the acid value of high acid value animal-plant oil is at 10～150mgKOH/g oil, according to the acid value difference, the add-on of glycerine and the mol ratio of the free fatty acids in the oil are 0.35～2.0, add strong acid simultaneously as catalyzer, add binary azeotropic solvent distillation or ternary azeotropic solvent distillation again, the add-on of azeotropic distillation solvent is 15～60% of high acid value animal-plant oil by weight
(2) stirring heating is carried out back flow reaction, the moisture that reaction generates is taken out of by azeotropic distillation solvent, and water separates automatically with solvent after the condensation, and azeotropic distillation solvent refluxes back in the conversion unit, water is then discharged, take reactor reaction out of until no moisture and finish, steam azeotropic distillation solvent, get esterification mixture, back flow reaction is carried out under normal pressure, the back flow reaction temperature depends on the azeotropic distillation solvent of employing between 60～120 ℃
(3) with after esterification mixture and the catalyst separating, adopt discoloring agent to the esterification mixture processing of decolouring then,
(4) esterification mixture after the decolouring, the amount of corresponding esterification mixture adds 15～30% methyl alcohol by weight, and 0.5～1.2% alkali catalyst is 60～80 ℃ in temperature and carries out transesterification,
(5) mixture that obtains of transesterification adopts centrifugation to go out raw glycerine, and raw glycerine is after acidifying separates, and the glycerine that part contains free fatty acids returns the esterification that esterifier is participated in process (1), and most of raw glycerine carries out glycerine and reclaims,
(6) fatty acid methyl ester after the separation of glycerin removes the free glycerol of trace with 30～45% hot wash, superfluous unreacted methanol is also dissolved in the water and is taken out of, centrifugation must be washed fatty acid methyl ester, the water of separating distills out methyl alcohol and returns the methyl alcohol storage tank, and the hot wash temperature is controlled at 60～95 ℃.
2, by the described high acid value animal-plant oil production method of bio-diesel oil of utilizing of claim 1, it is characterized in that the washing fatty acid methyl ester is carried out winterization in the winterization machine, the winterization temperature is-5～3 ℃, separates the high melting-point material after the winterization, obtains purified fatty acid methyl ester.
3, by claim 1 or the 2 described high acid value animal-plant oil production method of bio-diesel oil of utilizing, it is characterized in that described glycerine and free fatty acids mol ratio are 0.8～1.3.
4, by claim 1 or the 2 described high acid value animal-plant oil production method of bio-diesel oil of utilizing, it is characterized in that described strong acid is the vitriol oil of concentration 98%, add-on is 0.8～1.2% of high acid value animal-plant oil by weight, perhaps be macroporous type polystyrene storng-acid cation exchange resin, add-on is 5～10% of high acid value animal-plant oil by weight.
5,, it is characterized in that described binary azeotropic solvent distillation is benzene,toluene,xylene, hexanaphthene, pentane or the ethyl acetate that forms binary azeotrope with water by claim 1 or the 2 described high acid value animal-plant oil production method of bio-diesel oil of utilizing.
6,, it is characterized in that the ethanol and the hexanaphthene of the ternary azeotropic compositions that described ternary azeotropic solvent distillation forms for the ethanol of the ternary azeotropic compositions that forms with water and benzene or with water by claim 1 or the 2 described high acid value animal-plant oil production method of bio-diesel oil of utilizing.
7, by claim 1 or the 2 described high acid value animal-plant oil production method of bio-diesel oil of utilizing, it is characterized in that the more excellent scope of azeotropic distillation solvent add-on is 25～40%.
8, by claim 1 or the 2 described high acid value animal-plant oil production method of bio-diesel oil of utilizing, the discoloring agent that adopts that it is characterized in that decolouring is atlapulgite or activated carbon.
9, by the described high acid value animal-plant oil production method of bio-diesel oil of utilizing of claim 1, its described alkali catalyst is sodium methylate, NaOH or KOH, adopts NaOH, KOH to make alkali catalyst and should adopt its solid and dissolve in methyl alcohol in advance that to make alkali concn be 5～8% methanol solution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101116967A CN1238468C (en) | 2003-12-31 | 2003-12-31 | Production method of biodiesel oil using high acid ralue animal and vegetable grease |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101116967A CN1238468C (en) | 2003-12-31 | 2003-12-31 | Production method of biodiesel oil using high acid ralue animal and vegetable grease |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1556174A true CN1556174A (en) | 2004-12-22 |
| CN1238468C CN1238468C (en) | 2006-01-25 |
Family
ID=34336270
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2003101116967A Expired - Fee Related CN1238468C (en) | 2003-12-31 | 2003-12-31 | Production method of biodiesel oil using high acid ralue animal and vegetable grease |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1238468C (en) |
Cited By (26)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2007068137A1 (en) * | 2005-11-17 | 2007-06-21 | The Chinese University Of Hong Kong | The process for preparing biodiesel |
| CN1325606C (en) * | 2005-08-19 | 2007-07-11 | 华南理工大学 | Method for biocatalyzing ester exchange reaction of high acid value lipid to produce biodiesel oil |
| CN100335594C (en) * | 2005-02-24 | 2007-09-05 | 浙江工业大学 | Method for preparing biological diesel oil |
| CN100344732C (en) * | 2005-07-06 | 2007-10-24 | 中国科学院山西煤炭化学研究所 | Method of making biodiesel oil by subcritical methanol phase solid acid alkali catalytic oil fat ester exchange |
| CN100362082C (en) * | 2006-01-18 | 2008-01-16 | 马德扬 | Method for preparing biological diesel oil by utilizing animal oil |
| CN100365100C (en) * | 2005-08-01 | 2008-01-30 | 江苏工业学院 | Method of preparing biological diesel oil by methanol critical low alkali process |
| CN100372915C (en) * | 2006-06-15 | 2008-03-05 | 南京工业大学 | Process of preparing biological diesel by microchannel reactor |
| CN100386407C (en) * | 2006-06-12 | 2008-05-07 | 大连理工大学 | Process of producing biological diesel by high acid waste oil |
| CN100398629C (en) * | 2006-09-29 | 2008-07-02 | 合肥工业大学 | Technological process of preparing biological diesel oil with vegetable oil niger |
| CN100429291C (en) * | 2006-09-15 | 2008-10-29 | 王新俊 | Method of preparing biological diesel oil by peanut oil foot |
| CN100434164C (en) * | 2006-07-10 | 2008-11-19 | 张冰青 | Catalyst system and biological diesel oil producing process with the catalyst system |
| CN1974724B (en) * | 2006-12-04 | 2010-09-29 | 李燕丽 | High efficiency preparation process of biological diesel oil |
| CN101880602A (en) * | 2010-06-17 | 2010-11-10 | 暨南大学 | Method for preparing biodiesel by using high acid value oil |
| CN101245252B (en) * | 2007-02-14 | 2011-10-26 | 南京工业大学 | Method for producing biological diesel oil by using waste oil |
| CN102465058A (en) * | 2010-11-04 | 2012-05-23 | 朱建军 | Production process for preparing biodiesel |
| CN102517155A (en) * | 2011-12-14 | 2012-06-27 | 清华大学 | Method for combined production of cracked biodiesel and activated carbon |
| CN102559377A (en) * | 2011-08-16 | 2012-07-11 | 中国海洋石油总公司 | Washing tower heating method, biodiesel crude product washing method, and biodiesel preparation method |
| CN102656253A (en) * | 2009-12-23 | 2012-09-05 | 环球油品公司 | Low water biomass-derived pyrolysis oil and processes for preparing the same |
| CN102698800A (en) * | 2012-05-04 | 2012-10-03 | 凯瑞化工股份有限公司 | Resin catalyst for producing fatty acid methyl ester from high-acid-value oil |
| CN102816645A (en) * | 2012-09-14 | 2012-12-12 | 天津工业大学 | Continuous preparation method of biodiesel |
| CN103122278A (en) * | 2013-03-07 | 2013-05-29 | 中国石油大学(华东) | Preparation method of biodiesel |
| CN105154240A (en) * | 2015-08-10 | 2015-12-16 | 苏州丰倍生物科技有限公司 | Method for producing environment-friendly fatty acid methyl ester with glycerol method |
| CN107459997A (en) * | 2017-07-21 | 2017-12-12 | 中国林业科学研究院林产化学工业研究所 | A kind of high acid value waste oil glycerine is without catalytic esterification deacidification continuous production technology |
| CN114214121A (en) * | 2021-12-14 | 2022-03-22 | 浙江东江能源科技有限公司 | High-quality low-sulfur-content biodiesel preparation device and preparation method |
| CN114717056A (en) * | 2022-04-25 | 2022-07-08 | 广东省农业科学院农业质量标准与监测技术研究所 | Method for methyl esterification of oil by acid catalysis |
| US11851403B1 (en) | 2022-08-03 | 2023-12-26 | Inventure Renewables, Inc. | Processes and systems for improved alkyl ester production from feedstocks containing organic acids using low pressure alkylation |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101177617B (en) * | 2006-11-10 | 2010-11-10 | 北京化工大学 | Process for preparing biodiesel |
| CN100460484C (en) * | 2006-12-12 | 2009-02-11 | 周斌 | Process for lowering solidifying point of bio-diesel oil |
| CN102586512A (en) * | 2012-03-27 | 2012-07-18 | 陕西科技大学 | Method for reducing acid value of wild pepper seed oil and modifying wild pepper seed oil to prepare succinate sulfonate greasing agent |
-
2003
- 2003-12-31 CN CNB2003101116967A patent/CN1238468C/en not_active Expired - Fee Related
Cited By (30)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100335594C (en) * | 2005-02-24 | 2007-09-05 | 浙江工业大学 | Method for preparing biological diesel oil |
| CN100344732C (en) * | 2005-07-06 | 2007-10-24 | 中国科学院山西煤炭化学研究所 | Method of making biodiesel oil by subcritical methanol phase solid acid alkali catalytic oil fat ester exchange |
| CN100365100C (en) * | 2005-08-01 | 2008-01-30 | 江苏工业学院 | Method of preparing biological diesel oil by methanol critical low alkali process |
| CN1325606C (en) * | 2005-08-19 | 2007-07-11 | 华南理工大学 | Method for biocatalyzing ester exchange reaction of high acid value lipid to produce biodiesel oil |
| WO2007068137A1 (en) * | 2005-11-17 | 2007-06-21 | The Chinese University Of Hong Kong | The process for preparing biodiesel |
| CN100362082C (en) * | 2006-01-18 | 2008-01-16 | 马德扬 | Method for preparing biological diesel oil by utilizing animal oil |
| CN100386407C (en) * | 2006-06-12 | 2008-05-07 | 大连理工大学 | Process of producing biological diesel by high acid waste oil |
| CN100372915C (en) * | 2006-06-15 | 2008-03-05 | 南京工业大学 | Process of preparing biological diesel by microchannel reactor |
| CN100434164C (en) * | 2006-07-10 | 2008-11-19 | 张冰青 | Catalyst system and biological diesel oil producing process with the catalyst system |
| CN100429291C (en) * | 2006-09-15 | 2008-10-29 | 王新俊 | Method of preparing biological diesel oil by peanut oil foot |
| CN100398629C (en) * | 2006-09-29 | 2008-07-02 | 合肥工业大学 | Technological process of preparing biological diesel oil with vegetable oil niger |
| CN1974724B (en) * | 2006-12-04 | 2010-09-29 | 李燕丽 | High efficiency preparation process of biological diesel oil |
| CN101245252B (en) * | 2007-02-14 | 2011-10-26 | 南京工业大学 | Method for producing biological diesel oil by using waste oil |
| CN102656253A (en) * | 2009-12-23 | 2012-09-05 | 环球油品公司 | Low water biomass-derived pyrolysis oil and processes for preparing the same |
| CN101880602A (en) * | 2010-06-17 | 2010-11-10 | 暨南大学 | Method for preparing biodiesel by using high acid value oil |
| CN101880602B (en) * | 2010-06-17 | 2012-11-21 | 暨南大学 | Method for preparing biodiesel by using high acid value oil |
| CN102465058A (en) * | 2010-11-04 | 2012-05-23 | 朱建军 | Production process for preparing biodiesel |
| CN102559377A (en) * | 2011-08-16 | 2012-07-11 | 中国海洋石油总公司 | Washing tower heating method, biodiesel crude product washing method, and biodiesel preparation method |
| CN102517155A (en) * | 2011-12-14 | 2012-06-27 | 清华大学 | Method for combined production of cracked biodiesel and activated carbon |
| CN102698800A (en) * | 2012-05-04 | 2012-10-03 | 凯瑞化工股份有限公司 | Resin catalyst for producing fatty acid methyl ester from high-acid-value oil |
| CN102698800B (en) * | 2012-05-04 | 2014-05-14 | 凯瑞化工股份有限公司 | Resin catalyst for producing fatty acid methyl ester from high-acid-value oil |
| CN102816645A (en) * | 2012-09-14 | 2012-12-12 | 天津工业大学 | Continuous preparation method of biodiesel |
| CN103122278A (en) * | 2013-03-07 | 2013-05-29 | 中国石油大学(华东) | Preparation method of biodiesel |
| CN105154240A (en) * | 2015-08-10 | 2015-12-16 | 苏州丰倍生物科技有限公司 | Method for producing environment-friendly fatty acid methyl ester with glycerol method |
| CN107459997A (en) * | 2017-07-21 | 2017-12-12 | 中国林业科学研究院林产化学工业研究所 | A kind of high acid value waste oil glycerine is without catalytic esterification deacidification continuous production technology |
| CN114214121A (en) * | 2021-12-14 | 2022-03-22 | 浙江东江能源科技有限公司 | High-quality low-sulfur-content biodiesel preparation device and preparation method |
| CN114214121B (en) * | 2021-12-14 | 2024-02-20 | 浙江东江能源科技有限公司 | Preparation device and preparation method of high-quality low-sulfur biodiesel |
| CN114717056A (en) * | 2022-04-25 | 2022-07-08 | 广东省农业科学院农业质量标准与监测技术研究所 | Method for methyl esterification of oil by acid catalysis |
| CN114717056B (en) * | 2022-04-25 | 2023-07-18 | 广东省农业科学院农业质量标准与监测技术研究所 | Method for acid-catalyzed methyl esterification of grease |
| US11851403B1 (en) | 2022-08-03 | 2023-12-26 | Inventure Renewables, Inc. | Processes and systems for improved alkyl ester production from feedstocks containing organic acids using low pressure alkylation |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1238468C (en) | 2006-01-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1238468C (en) | Production method of biodiesel oil using high acid ralue animal and vegetable grease | |
| CN1041822C (en) | Process for the continuous production of C1 to C4 alcyl esters of higher fatty acids | |
| US8728177B2 (en) | Production of biodiesel and glycerin from high free fatty acid feedstocks | |
| CN101198677B (en) | Method and equipment for producing fatty acid alkyl-ester by using fatty acid | |
| US20100331558A1 (en) | Method for producing fatty acid methyl ester | |
| CN102465058A (en) | Production process for preparing biodiesel | |
| AU2004324250A1 (en) | Improved process for the preparation of fatty acid methyl ester (Biodiesel) from triglyceride oil through transesterification | |
| CN1900223A (en) | Method for conitinuously producing biological diesel oil using solid acid catalyst and piston flow reactor | |
| CN1303187C (en) | Method for synthesizing biodiesel utilizing swill water oil | |
| WO2004048311A1 (en) | Method for production of alkyl esters | |
| JP4920583B2 (en) | Fatty acid lower alkyl ester and light oil alternative fuel | |
| CA2637799A1 (en) | Method for obtaining fuels from vegetable and animal fat waste and installation for carrying out said method | |
| CN1844319A (en) | Process for preparing bio- diesel oil by conversion of subcritical - supercritical fluid | |
| CN101338214B (en) | Method for preparing biodiesel using acidizing oil as raw material under normal pressure | |
| CN1861752A (en) | Process of producing biological diesel by high acid waste oil | |
| CN1670128A (en) | Process for preparing biological diesel oil by using waste oil | |
| CN100355860C (en) | Process for preparing bio- diesel oil by two-step catalysis of acid-containing fat | |
| CN1923990A (en) | Process for preparing fatty acid ester | |
| CN1786117A (en) | Method of preparing biological diesel oil by methanol critical low alkali process | |
| US9725397B2 (en) | Production of biodiesel and glycerin from high free fatty acid feedstocks | |
| CN101544928B (en) | Method for reducing acid value of bio-oil materials | |
| CN101486923A (en) | Environment friendly process for biodiesel | |
| JP5637484B2 (en) | Raw material fats and oils for producing higher fatty acid alkyl esters and method for producing higher fatty acid alkyl esters | |
| CN103374463B (en) | Preparation method of biodiesel | |
| TWI297357B (en) | System for continuously producing biodiesel |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: WUHAN AIRUI BIOLOGICAL DIESEL CO., LTD. Free format text: FORMER NAME OR ADDRESS: INST. OF OIL CROPS, CHINESE ACADEMY OF AGRICULTURE |
|
| CP03 | Change of name, title or address |
Address after: 430070 Hubei Province, Wuhan city Hongshan District Luoshi Road No. 517 Ming Ze building 19 floor Patentee after: Wuhan Rui Rui bio diesel Co., Ltd. Address before: 430062 No. two, 2 Dong Lu, Wuchang District, Hubei, Wuhan Patentee before: Inst. of Oil Crops, Chinese Academy of Agricultural Scences |
|
| ASS | Succession or assignment of patent right |
Owner name: INST. OF OIL CROPS, CHINESE ACADEMY OF AGRICULTURE Free format text: FORMER OWNER: WUHAN AIRUI BIO-DIESEL CO., LTD. Effective date: 20090619 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20090619 Address after: 2, No. two, Dong Xu Road, Wuchang District, Hubei, Wuhan Patentee after: Inst. of Oil Crops, Chinese Academy of Agricultural Scences Address before: Hubei city of Wuhan province Luo Shi Road Hongshan District No. 517 Ming Ze building 19 floor Patentee before: Wuhan Rui Rui bio diesel Co., Ltd. |
|
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20060125 Termination date: 20161231 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |